CN205061885U - Carbon dioxide conversion device - Google Patents
Carbon dioxide conversion device Download PDFInfo
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- CN205061885U CN205061885U CN201520841517.3U CN201520841517U CN205061885U CN 205061885 U CN205061885 U CN 205061885U CN 201520841517 U CN201520841517 U CN 201520841517U CN 205061885 U CN205061885 U CN 205061885U
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- gas
- carbon dioxide
- conversion device
- dioxide conversion
- reaction
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Abstract
The utility model relates to the technical field of chemical equipment, especially relate to carbon dioxide conversion device, include: the cavity evenly is provided with the reaction tube of wearing to establish the cavity in a plurality of both ends in, be provided with catalyst layer and backup pad in the reaction tube, the reaction tube both ends are connected with give vent to anger collecting pipe and raw materials input piece respectively, raw materials input piece includes: feed gas distribution district and feed gas are imported, and the raw materials is imported the piece and is used for after the feed gas is distinguished by the distribution of feed gas import incoming stock gas, and the district is mixed in the feed gas distribution, gets into the reaction tube after mixing, anti - living reaction in the reaction tube, and the gas of reaction back formation is by the collecting pipe collection of giving vent to anger, the cavity is provided with the piece that burns in the collecting pipe one end of giving vent to anger, and the burning piece comprises fuel gas entry and burner nozzle, and burner nozzle enters the mouth near fuel gas and sets up. Above -mentioned carbon dioxide conversion device, it provides the reaction temperature of heat in order to provide the reaction tube to be burnt by flammable fuel gas through the burning piece, and be safe swift.
Description
Technical field
The utility model relates to technical field of chemical, particularly relates to a kind of carbon dioxide conversion device.
Background technology
Traditional is technical, carbon monoxide and be always the basic raw material of organic chemical industry and fine chemistry industry containing the synthetic gas of carbon monoxide, in full ten-million-ton scale methanol production, millions of tonnes carbonyl synthesis acetic acid, aceticanhydride, the ethylene glycol production etc. of ton, the fuel oil production etc. of millions of tons.In the whole world, the source of carbon monoxide mainly has Sweet natural gas gas and gas maked coal production to obtain.Along with the Chinese government industrial adjustment, environmental protection and clean energy enforcement, country support energetically Sweet natural gas the most domestic fuel be suitable for, the new project utilizing Sweet natural gas to prepare carbon monoxide has been subject to country's restriction gradually.Therefore, the most in recent years, gas maked coal technology had become the main technological route of synthesis carbon monoxide or synthetic gas.But although China is coal big country, coal is a kind of limited resources after all, simultaneously in gas maked coal device, the environmentally harmful by product of a large amount of associations can be produced, process these nuisances and also will waste more resource.Effectively utilize coal resources, concern the important thing of national economic development and environment protection.
In addition, because the many industries of China use coal source in a large number, the carbonic acid gas of China's discharge is caused to occupy first place, the whole world.The responsibility of the harm that Greenhouse effect bring and environment protection has required that country must energy-saving and emission-reduction in development.The exploitation of technology that utilizes of carbonic acid gas has become whole world research hot topic.As the exploitation of carbonic acid gas methane technology, carbonic acid gas prepare polycarbonate etc.
Because hydrogen is that a kind of human future world may rely on the larger energy, because it can derive from materials maximum on the earth---water, inexhaustible.The many industries of current China, the enterprise's by-product by-product tail gas in a large number containing hydrogen, as the coke(oven)gas of iron and steel enterprise, polysilicon reproduce gas, production of styrene tail gas, chlor-alkali industry produce in by-product hydrogen, refinery tail-gas etc., these are rich in the tail gas of hydrogen, reach 1,600 hundred million M3 every year at the generation of China.Although effectively isolated hydrogen recycling through membrane separation technique and PSA Technology, applied limited, only have 30% measure efficiency utilization, great majority employ as fuel.And hydrogen is inflammable and explosive hazardous chemical, not easily transport for long-distance, preferably utilize nearby, due to these restrictions, many enterprises are only had unnecessary secondary hydrogen emptying or burning are used as steam use, its effective value is not embodied, according to calculating 10 ~ 20 times that the value of hydrogen as the prepared using of chemical is its value as fuel steam.
If carbonic acid gas can be used, it is allowed to synthesize carbon monoxide with the tail gas being rich in hydrogen, so both reduce the discharge of carbonic acid gas, the by-product tail gas that can make again to be rich in hydrogen uses for industrial chemicals as far as possible, can reduce the consumption of Sweet natural gas in Sweet natural gas gas and gas maked coal or coal to a certain extent.Therefore can say this technology once application, will be the new Prospect of Gasification Technology of except Sweet natural gas or gas maked coal technology except one, invests that to reduce costs be all favourable in energy-saving and emission-reduction and reducing.
Present market is upper, and domestic seldom have the technical literature of the industrialized unit and equipment synthesizing carbon monoxide about hydrogenation of carbon dioxide to report.
The technology that patent of invention 200510027918.6 discloses under the environment of anaerobic, makes reductive agent Reactive Synthesis carbon monoxide with carbonic acid gas with coke, its reactor used is fixed-bed reactor, adopt the mode of coal self-burning in reaction bed, be not shell and tube reactor structure, concrete structure of reactor is not discussed.
The technology that patent of invention 200810046409.1 discloses is the processing method of carbonic acid gas and hydrogen synthesizing methanol, and because its synthesis temperature is lower than 300 DEG C, the reactor of employing does not need fuel combustion or high temperature heat exchange.Therefore, its reactor can not be used by Suitable carbon dioxide hydrogenation synthesis carbon monoxide.
But, the convertor of coke(oven)gas synthesis carbon monoxide, use temperature is at 850 ~ 1000 DEG C, and the form of employing is after unstripped gas passes into, directly have the oxygen or oxygen enrichment that pass into and burn as the coke(oven)gas of unstripped gas and material heat is provided, but this combustion system carries out in reaction bed.If the situations such as distortion, blocking, damage appear in burner, easily occur that oxygen combustion is incomplete, owing to containing a large amount of hydrogen in coke(oven)gas, easily occur blast.In fact just occurred at home that such reactor exploded due to the reason of burner.
Utility model content
Based on this, be necessary, for how solving existing reactor because heating the problem of easily blasting in reaction bed combustion, to provide a kind of carbon dioxide conversion device.
A kind of carbon dioxide conversion device, comprising: chamber, is evenly provided with the reaction tubes that multiple two ends wear described chamber in described chamber; Be provided with catalyst layer and back up pad in described reaction tubes, the described catalyst layer in described back up pad is for loading catalyzer; Described reaction tubes two ends are connected to give vent to anger collection tube and raw material input component; Described raw material input component comprises: unstripped gas distribution zone and raw material gas inlet, described raw material input component is used for after unstripped gas is by the incoming stock gas distribution zone of raw material gas inlet, mix in described unstripped gas distribution zone, described reaction tubes is entered after mixing, anti-raw reaction in described reaction tubes, the gas generated after reaction is collected by described collection tube of giving vent to anger; Described chamber is provided with burner element in described collection tube one end of giving vent to anger, and described burner element is made up of fuel gas entrance and burner noz(zle), and described burner noz(zle) is arranged near described fuel gas entrance.
Wherein in an embodiment, the quantity of described burner noz(zle) is two.
Wherein in an embodiment, two described burner noz(zle)s are 30-50mm apart from the distance of described reaction tubes.
Wherein in an embodiment, two described burner noz(zle)s are 40mm apart from the distance of described reaction tubes.
Wherein in an embodiment, described fuel gas entrance is also provided with capping, for cutting off being communicated with of described fuel gas entrance and described chamber.
Wherein in an embodiment, described chamber offers nitrogen inlet and steam entry in the near zone of described burner noz(zle).
Wherein in an embodiment, described chamber offers smoke outlet and smoke inlet, and described smoke inlet is for connecting outside high hot flue gases, and described smoke outlet is for discharging the flue gas after utilization.
Wherein in an embodiment, described chamber inner side-wall is provided with thermosphere.
Wherein in an embodiment, the diameter of described reaction tubes is at φ 40-201mm.
Wherein in an embodiment, described reaction tube diameter is 201mm.
Above-mentioned carbon dioxide conversion device, provides heat to provide the temperature of reaction of reaction tubes by burner element by ignitable fuel gas firing, safe and efficient.
The high temperature resistant stainless steel pipe that reaction tubes is selected, can resistance to temperature 900 ~ 1000 DEG C, even if external heat temperature local reaches the operation that more than 750 DEG C do not affect reaction tubes yet.
Nitrogen or water vapour tube inlet are installed, danger can be processed in time, timely fire extinguishing cooling.
This device adopts burning external heat, and compared with reaction bed combustion technology, explosion hazard reduces greatly.
Accompanying drawing explanation
Fig. 1 is the structural representation of carbon dioxide conversion device of the present utility model;
Fig. 2 is cross-sectional schematic embodiment illustrated in fig. 1;
Fig. 3 is the distribution schematic diagram of reaction tubes embodiment illustrated in fig. 1.
Embodiment
For enabling above-mentioned purpose of the present utility model, feature and advantage become apparent more, are described in detail embodiment of the present utility model below in conjunction with accompanying drawing.Set forth a lot of detail in the following description so that fully understand the utility model.But the utility model can be much different from alternate manner described here to implement, those skilled in the art can when doing similar improvement without prejudice to when the utility model intension, and therefore the utility model is by the restriction of following public specific embodiment.
It should be noted that, when element is called as " being fixed on ", " being arranged at " another element, directly can there is element placed in the middle in it on another element or also.When an element is considered to " connection " another element, it can be directly connected to another element or may there is centering elements simultaneously.Term as used herein " vertical ", " level ", "left", "right" and similar statement just for illustrative purposes, do not represent it is unique embodiment.
See also Fig. 1, Fig. 2 and Fig. 3, carbon dioxide conversion device, comprising: chamber 100, and its aspect ratio is 6.The reaction tubes 110 that multiple two ends wear described chamber 100 is evenly provided with in described chamber 100.Such as, described chamber 100 two ends offer multiple installing port, for installing described reaction tubes 110.
Such as, the diameter of reaction tubes 110 is 120mm.Be provided with catalyst layer 111 and back up pad 112 in reaction tubes 100, catalyst filling is in back up pad 112.Reaction tubes 110 two ends are connected to give vent to anger collection tube 130 and raw material input component 140.
Such as, raw material input component 140 comprises: unstripped gas distribution zone 141 and raw material gas inlet 142.Unstripped gas, by after the incoming stock gas distribution zone 141 of raw material gas inlet 142, mixes in unstripped gas distribution zone 141, enters reaction tubes 110 after mixing, and anti-raw reaction in reaction tubes 110, the gas generated after reaction is collected by collection tube 130 of giving vent to anger.
Such as, collection tube 130 of giving vent to anger also connects collected outside equipment by airway, so that export the gas generated after reaction to collected outside equipment.
Such as, chamber 100 is provided with burner element in described collection tube 130 one end of giving vent to anger, and burner element is made up of fuel gas entrance 151 and two burner noz(zle)s 152, and described burner noz(zle) is arranged near described fuel gas entrance.
Such as, fuel gas entrance 151 is also provided with capping 1511, for being communicated with of fuel shutoff gas entrance 151 and chamber 100.
Such as, multiple reaction tubes 110 is arranged on equably along the region near described chamber 100 inwall 10mm.
Such as, unstripped gas treatment capacity in order to ensure the homogeneous temperature of reaction tubes, in reaction tubes is at 5000M
3/ below h, and, ensure that reaction tube diameter is at φ 40-201mm.Reaction tube diameter is in 201mm, and can ensure the anti-uniformity of temperature profile needed of reaction in catalyst layer 111, temperature of reaction is beneficial to control, controls unstripped gas treatment capacity at 5000M
3/ below h, to ensure that the temperature in chamber 100 controls at 500-800 DEG C, so, ensures normally carrying out of reaction, avoids meeting accident.
In order to control temperature of reaction further, such as, two burner noz(zle)s 152 are 30-50mm apart from the distance of reaction tubes 110.Such as, two burner noz(zle)s 152 are 30mm apart from the distance of reaction tubes 110.Such as, two burner noz(zle)s 152 are 50mm apart from the distance of reaction tubes 110.Such as, two burner noz(zle)s 152 are 40mm apart from the distance of reaction tubes 110.So, ensure the anti-uniformity of temperature profile needed of reaction in catalyst layer 111, temperature of reaction is beneficial to control.
In order to avoid at the too high damage reaction tubes of reaction process middle chamber temperature, such as, near burner noz(zle), offer nitrogen inlet 153 and steam entry 154.Water vapour and nitrogen inlet are installed near burner noz(zle), nitrogen extinguishing can be passed into rapidly when cavity occurs dangerous, then pass into water vapour heat sink.So, avoid, at the too high damage reaction tubes of reaction process middle chamber temperature, even damaging whole device.
In embodiment in fact, also can not use burner element, and the temperature of reaction of reaction tubes 110 can be reached equally.Such as, chamber 100 offers smoke outlet 143 and smoke inlet 144.Smoke inlet 144 is for connecting outside high hot flue gases.Smoke outlet 143 is for discharging the flue gas after utilization.
In order to ensure normally carrying out of reaction, such as, chamber 100 inner side-wall is provided with thermosphere, and such as, refractory layer adopts high temperature material to make.Further, high temperature material tiles three layers and forms refractory layer.So, ensure that the fire-resistant high temperature of chamber 100.
Reaction principle:
Hydrogenation of carbon dioxide synthesis carbon monoxide technology, its chemical equation is: CO2+H2=CO+H2O.
The reaction of hydrogenation of carbon dioxide synthesis carbon monoxide is thermo-negative reaction, and obtain desirable carbon dioxide conversion and carbon monoxide selection rate, generally its temperature of reaction will more than 550 DEG C, preferably more than 600 DEG C.When temperature is lower than 550 DEG C, transformation efficiency can significantly reduce.Therefore, reaction needed heat of high temperature.This conversion system is designed in following two kinds of situations all applicable:
The first situation utilizes outer fuel and the air of supplying to provide heat in chamber combustion to reaction tubes.The fuel used comprises Sweet natural gas, coal gas, coke(oven)gas, hydrogen, oil liquefied gas and is rich in the fuel gas etc. that can contaminate material.Ignition dope, directly extracts the air in environment, regulates by air dampers.Lighter for ignition, burner noz(zle) is provided with in chamber.After fuel combustion, the heat of generation by radiation section to the multiple reaction tubes heat supplies being filled with catalyzer.
The second situation relies on high hot flue gases directly and reaction tube heat exchange, do not need the function employing burner noz(zle).The utility model is mainly applied to Sweet natural gas, coal gas, coke(oven)gas, hydrogen, oil liquefied gas and is rich in the enterprise of fuel gas of combustiblesubstance.Also be applicable to the enterprise that there is temperature and be greater than the high hot flue gases of more than 700 DEG C, as Steel Plant, cement mill etc., rely on high-temperature flue gas directly and reaction tubes heat exchange, can part of fuel be saved.
Working process:
When using fuel gas burning, close high hot flue gases entrance.When using high hot flue gases heat exchange, close capping, the burner noz(zle) spare time is used.Near burner noz(zle), nitrogen or steam-in are being installed, in case when occurring dangerous in convertor, pass into nitrogen or the rapid fire extinguishing cooling of water vapour.On convection zone top, unstripped gas entrance is installed, enters after carbonic acid gas and hydrogen are pre-mixed.Raw material gas inlet is provided with pipe type heat transfer, and for the preheating of unstripped gas, the unstripped gas after preheating just enters through the gas service pipes being installed on product distribution district the reaction tubes being installed on chamber.And reacted reforming gas is got rid of through collection tube of giving vent to anger.Preferably, reaction tubes is high temperature resistant stainless steel pipe, use temperature 900-1000 DEG C.
Each technical characteristic of the above embodiment can combine arbitrarily, for making description succinct, the all possible combination of each technical characteristic in above-described embodiment is not all described, but, as long as the combination of these technical characteristics does not exist contradiction, be all considered to be the scope that this specification sheets is recorded.
The above embodiment only have expressed several embodiment of the present utility model, and it describes comparatively concrete and detailed, but therefore can not be interpreted as the restriction to utility model patent scope.It should be pointed out that for the person of ordinary skill of the art, without departing from the concept of the premise utility, can also make some distortion and improvement, these all belong to protection domain of the present utility model.Therefore, the protection domain of the utility model patent should be as the criterion with claims.
Claims (10)
1. a carbon dioxide conversion device, is characterized in that,
Comprise: chamber, in described chamber, be evenly provided with the reaction tubes that multiple two ends wear described chamber;
Be provided with catalyst layer and back up pad in described reaction tubes, the described catalyst layer in described back up pad is for loading catalyzer;
Described reaction tubes two ends are connected to give vent to anger collection tube and raw material input component;
Described raw material input component comprises: unstripped gas distribution zone and raw material gas inlet, described raw material input component is used for after unstripped gas is by the incoming stock gas distribution zone of raw material gas inlet, mix in described unstripped gas distribution zone, described reaction tubes is entered after mixing, anti-raw reaction in described reaction tubes, the gas generated after reaction is collected by described collection tube of giving vent to anger;
Described chamber is provided with burner element in described collection tube one end of giving vent to anger, and described burner element is made up of fuel gas entrance and burner noz(zle), and described burner noz(zle) is arranged near described fuel gas entrance.
2. carbon dioxide conversion device according to claim 1, is characterized in that, the quantity of described burner noz(zle) is two.
3. carbon dioxide conversion device according to claim 1, is characterized in that, two described burner noz(zle)s are 30-50mm apart from the distance of described reaction tubes.
4. carbon dioxide conversion device according to claim 1, is characterized in that, two described burner noz(zle)s are 40mm apart from the distance of described reaction tubes.
5. carbon dioxide conversion device according to claim 1, is characterized in that, described fuel gas entrance is also provided with capping, for cutting off being communicated with of described fuel gas entrance and described chamber.
6. carbon dioxide conversion device according to claim 1, is characterized in that, described chamber offers nitrogen inlet and steam entry in the near zone of described burner noz(zle).
7. carbon dioxide conversion device according to claim 1, is characterized in that, described chamber offers smoke outlet and smoke inlet, and described smoke inlet is for connecting outside high hot flue gases, and described smoke outlet is for discharging the flue gas after utilization.
8. carbon dioxide conversion device according to claim 1, is characterized in that, described chamber inner side-wall is provided with thermosphere.
9. carbon dioxide conversion device according to claim 1, is characterized in that, the diameter of described reaction tubes is at φ 40-201mm.
10. carbon dioxide conversion device according to claim 1, is characterized in that, described reaction tube diameter is 201mm.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201520841517.3U CN205061885U (en) | 2015-10-28 | 2015-10-28 | Carbon dioxide conversion device |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201520841517.3U CN205061885U (en) | 2015-10-28 | 2015-10-28 | Carbon dioxide conversion device |
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| Publication Number | Publication Date |
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| CN205061885U true CN205061885U (en) | 2016-03-02 |
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| Application Number | Title | Priority Date | Filing Date |
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| CN201520841517.3U Expired - Fee Related CN205061885U (en) | 2015-10-28 | 2015-10-28 | Carbon dioxide conversion device |
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105861055A (en) * | 2016-06-07 | 2016-08-17 | 太原理工大学 | Reaction device for preparing synthesis gas through catalytic reforming of methane and carbon dioxide |
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2015
- 2015-10-28 CN CN201520841517.3U patent/CN205061885U/en not_active Expired - Fee Related
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105861055A (en) * | 2016-06-07 | 2016-08-17 | 太原理工大学 | Reaction device for preparing synthesis gas through catalytic reforming of methane and carbon dioxide |
| CN105861055B (en) * | 2016-06-07 | 2019-01-22 | 太原理工大学 | The reaction unit of synthesis gas is prepared for methane and carbon dioxide catalytic reforming |
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Legal Events
| Date | Code | Title | Description |
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| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| CF01 | Termination of patent right due to non-payment of annual fee |
Granted publication date: 20160302 Termination date: 20161028 |
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| CF01 | Termination of patent right due to non-payment of annual fee |